Obtaining motor-spirit and burning-oil from higher-boiling petroleum



H. P. GHAMBERLAIN.

OBTAINING MOTOR SPIRIT AND BURNING OIL FROM HIGHER BOILING PETROLEUM.

APPLICATION man Aue. 11, 191s.

Patented Dec. 13, 1921;

H. P. CHAMBERLAIN. OBTAINING MOTOR SPIRIT AND BURNING OIL FROM HIGHERBOILING PETROLEUM.

APPLICATION FILED AUGJ IT 1916.

Patented Deu. 13, 1921.

4 SHEETS-SHEET 2.

l H. P. CHAMBERLAIN. OBTAINING MOTOR SPIRIT AND BURNING-OIL FROM HIGHER BOILING PETROLEUM. APPLICATION man Auw?. 191s.

Patented Dec. 13, 1921.

4 SHEETS-SHEET 3.

| Tessa-@az osgmszc'zhz 5275/@ Bruner-EBV pm L /4 @WMM n GI'fIfornug H. P. CHAMBERLAIN.

OBTAINING MOTR SPIRIT AND BURNING OIL FROM HIGHER BOILINGPETROLEUM.

APPLICATION FILED AUG. ITI 1916.

1,400,41 9. Patented Dec. 13, 1921.

' wll 4 SHEETS-SHEET 4.

m1700115* firm@ v 60 E I I I z sig/@771,3 F i I Burn/i OLZ mit UNITED STATES PATENT OFFICE.

HORACE P. CHAMBERLAIN, OF BUFFALO, NEVI YORK, ASSIGNOR TO STANDARD OIL COMPANY OF NEW YORK, OF NEW YORK. N. Y., A CORPORATION OF NEW YORK.

OBTAINING MOTOR-SPIRIT AND BURNING-GIL FROM HIGHER-BOILING PETROLEUM.

Specification of Letters Patent.

Patented Dec. 13, 1921.

Application led August 17, 1916. Serial No. 115,512.

To all tc/Lom may concern.'

Be it known that I, Hormon P. @iranienn- LAIN, citizen ot the United States, residing at Bul? lo, in the county oi Erie and ,State of New Yorlr, l are invented certain nen7 and useful improvements in Obtaining Motor- Sipirit and Burning-Uil from Higher-Bolling Petroleum, oi' which the following is a snecilication.

mrlhis invention relates more particularly to processes and apparatus whereby' (l) motor spirit or use in explosive engines and (2) burning oil (kerosene) for combustion in lamps with Wiclrs can be obtained by operations which include the decomposition or* hydrocarbons that have boiling points above 5*;80 F. (270O C.) Each ot' the improvements however which compose the invention is intended to be secured ior all the uses to which it may be applicable, severally or in combination and with or Without modilication.

Hydrocarbons with boiling points intermediate 3020 F. and 5180 (150o C. to 2700 C.) are regarded herein as normal to burning oil (kerosene). Motor spirit consists mainly of hydrocarbons with boiling points below 3020 F.; but it also contains some higher boiling hydrocarbons. lt is important that it should be volatile in its entirety below a `wrescribed temperature. This temperature ma y Yvary according to the grade of- L.

.i 7. product, it the present time a motor spirit would be merchantable it a sample thereof, subjected to distillation assay in the customary Way by means of a laboratory 'dash with side tube and a thermometer whose bulb is located in the flask neck just below said side tube, should all pass olf when or before say 3950 F. is attained; so that no appreciable quantity et oil should then remain in the assay flask. Percentages given herein for liquids are by Volume unless percer ge by' Weight should be stated.

The following procedure may Well be employed in order to carry the invention into etlgect .in a form which embodies (by Way of example) all of the improvements which compose said invention.

First. Petroleum in the crude form in which it is produced at the Wells, after separation ot Water and earthy matter by settling and decantation, is distilled in any lnoirn or suitable Way with collection (besides other distillates) ot one or more distillates, such as the customary Water White burning oil (kerosene) distillate and the succeeding mixed naphtha-burning-oil-gas-oil distillate, which consist largely of hydrocarbons with boiling points below 518O F., but which also contain a considerable percentage at least of those with boiling points above SiS@ F. and which are free (at least practically) trom hydrocarbons with viscosities normal for medium and heavy grades or' lubricants. The minimum Viscosity of hydrocarbons normal tor medium lubricants may be taken at one hundred and seventy seconds at i000 F. by an Engler viscosimeter, with Which Water -would exhibit a Viscosity of titty three seconds at 1000 F.

Second. Such distillates (best aftertreatment ot the same with sulfuric acid and separation of reaction products from the treated oil, but it may be without such treatment) are distilled (rerun) to dryness or as near thereto as preferred, in any known or suitable way `with collection separately of distinct distillates (twice run oils), one (at least) composed mainly of hydrocarbons with boiling points below 5180 F. and one other (at least) composed mainly ot hydrocarbons with boiling points above 518O F.

rlhird. The heavier ot' these twice run oils is subjected (by itself or in admixture with other appropriate oil) to distillation at decomposing temperatures under superatmosplieric pressure of more than thirty pounds, best about seventy-live pounds per square inch. ln the run hereinafter more particularly described, these temperatures ranged from 6960 F. to 7360 F., average about 713D F.

Fourth. ln this high pressure distillation the oil operated upon is appropriately heated in a compact body (say With an original volume or about rive thousand gallons as a minimum) .in a still oli appropriate size and strength (say with capacity of about one thousand cubic feet as a minimum and of a strength to withstand at said decomposing temperatures, With a proper margin of safety, said internal pressure of more than thirty pounds per square inch above atmospheric pressure), which still has its top exposed to the atmosphere to the extent of about one-third of its periphery in order that partialcondensation ot the evolved vapors may taire place in the vapor space overlying the oil in distillation in what is regarded as the best proportion to kbe eil'ected within the still. ln effecting this partial condensation the evolved vapors may be cooled about l5()O ll., more or less, say between one hundred degrees F. and two hundred degrees F. below the contemporaneous temperatures ot the oil in distillation. Preterably a still of horizontal cylindrical form with a capacity of upward ot three thousand cubic '.teet would be used; and the stock charged into such a still would best have an originalvolume 'ot lupward oi lifteen thousand gallons.

`ilth. rlhe condensate so termed within the vapor space ot the still is returned to the oil in distillation.

Sixth. rl`he uncondensed vapors pass out oi the still and are cooled in the 'torni of a single upwardly inclined stream, less than sixinches in diameter, elongated to more than one hundred times its diameter, and best exemplified by a :tour-inch stream eighty lecty long when a body ot petroleum with an original volume of about litteen thousand gallons is distilled as aforesaid.

Seventh. rllhe heat yconducting walls inclosingsaid stream (or streams) et vapors would best have an area oit air cooled surtace equal to about twenty per cent. (sayrbetween ten 'per cent. and thirty per cent.) of the exposed area of the still top and the cubic contents of the space occupied by said stream (or streams) would best be less than one and a half per cent. ot the original volume ot the still charge which would correspond with less than one per cent. olf the cubic contents of thestill; since normally the still wouldn e lilled about six-tenths tull at the beginning oit a run. The vapors may wellV be cooled therein about 900 ll., more or less, say between forty degrees l?. and one hundred and forty degrees J. below the contemporaneous temperatures ot' the vapors leaving the still.

Eighth. lThe condensate formed from said stream 'flows under and in contact with the oppositely flowing vapors and is returned to the oil in distillation alter thus altording an extended opportunity 'tor interchange ot hydrocarbons between itselil and the vapors.

Ninth. By' cooling the evolved vapors lirst inthe still and then in the outside 'upwardly inclined stream said vapors are reduced in temperature so 'liar below 5500 lt. (287.80 C.) that hydrocarbons with boiling points above vilSO F. (2700 C.) compose at most not more than about twenty live per cent. (measured in liquid state) ot the vapors passing onward and lso tar above i100 F. (23.00 C.) that upward oil' thirty live per cent. of hy drocarbons with boiling points above lill@ ll., including at least an appreciable amount ot said hydrocarbons with boiling points above 5180 ll., are contained in said vapors. Thus, a sample of the total oil obtainable iu a run trom conoensing said vapors in an ordinary water cooled condenser under atmospheric pressure should be subjected to a distillation assay, upward of thirty live per cent. oit the sample will remain in the assay liaslr at i100 F. and an appreciable quantity, but not so much as twenty live per cent., when lSO l?. isattained. ln the run hereinalter more particularly described, wherein the vapors passing onward from said'upwardly inclined stream had the composition just mentioned, the temperatures of the S0 same at this point ranged 'from about 4320 to about i980 ll., average about 455C F.

lhave 'discovered that when the liorni'ation ot condensate to be returned to the oil in distillation is thus restricted there are l`or equal volumes ot like oil operated upon, (l) less roi-mation ot' coltey in the still, (2) less consumption ot iluel, (3) less danger of over-` heating the still bottoni, and (l) less wear und tear generally on the still than there would be were a larger proportion orn the evolved vapors to be so returned; while at the same time the proportion ot distillate obtainable by condensation oic the then remaining vapors is enough larger and the qui/lity ot such distillate sutliciently good to malte the yield oli motor spirit oit' a given grade little interior (it not, in i'aet, equal or superior) to that obtained with said larger return of condensate to the oil in distilla- 100 tion.

Un the other hand,'should the formation ot condensate return to the oil in dist-illation be substantially more restricted a smaller amount ot hydrocarbons, available 105 tor use in motor spirit of a given grade,

would be .termed in the still; and the yield` ot' such motor spirit 'would consequently be reduced. y

ln this connection it is to be observed that the amount of such so available hydrocar` bons does not necessarily always increase union the evolved vapors are cooled for lor- :oiation oi a larger proportion et return con- Aay sometimes at least decrease; and it is .vell theretore, to adjust the coolin aOencies accordingly. 1

Tenth. lhe vapors that pass onward are partially condensed by bringing them into contact with the walls ot numerous parallel Y cooling pipes so arranged that said walls are interposed between currents of said vapors and oli aeri'rorin cooling fluid tlowing the iforiner over the outside and the latter through the interior ot said pipes; or conversely.

Eleventh. The conditions of 'partial condensation are so adjusted that the vapors which remain uncondensed therein are at li/.ly experience tends to show that '115 densed vapors had the composition just mentioi'ied, the temperatures of the same at this point ranged from about 267 F. to about S900 F., average about 341C' F.

Twelfth. The condensate formed by said Partial condensation is drawn off as dislt is hereinafter called the heavy distillate or simply the heavy stream. mteentli. The vapors then remaining unco densed are separately condensed by further cooling; and the so obtained condensate is drawn off as a distinct distillate. lt is hereinafter alled the light stream distillate, or simply the light stream. The total of collectible in a run would contain almost (if not quite) all of the distillate hydrocarbons with boiling points below 3020 while at the same time its content of obtaining, kby a single subsequent distillation thereof, a good yield of motor spirit hich would all of it distil over below a j fen merchantable temperature.

Villere either hydrocarbons with boiling points above liSO F. in considerable proportion. or an excessive percentage of hydrocarbons with boiling points above 410 F., to be present in said light stream, the amount of motor spirit of given grade, obtainable therefrom by a single distillabe diminished. li/loreover, and a large proportion of hydroboiling points above 5180 F.

wi were )resent in said light stream, increased exiienses iiould be sulfuric aci in operat inafter set incurred for fuel, plant, d and .other chemical reagents upon said light .stream as hereie other hand, were the percentage rbons in said lightstream with beve l-lOO F. to be unduly f en of a larger part vapors more of the total in these vapors with boiling ..20 F. would enter the heavy illate; a l the expense of getis subjected to a mild treatiric aci i; that is to say, it is t with sulfuric acid insuihcient in `i or in quantity to refine the heavier hydrocarbons thereof suitably for burning but the acid employed may be, and best we iid be, sufficient to refine the lighter hy- Sixteenth. The so separat-ed oil is distilled as long as the distillate is satisfactory/.f for motor spirit (or such other light product as may be desired). rllhe so obtained distillate may be a finished merchant-able article; or it may be (according` to the case) in condition to require further refining.

Seventeenth. The residual portion of the light stream (herein called light stream naphtha bottoms for convenience of reference) is distilled say as long as the distillate is of satisfactory quality for burning oil in view of subsequent operations to be performed on said distillate.

Eighteenth. The so obtained distillate (herein called light stream burning oil distillate) is treated with sulfuric acid; and the so treated oil is separated from reaction products.

Nineteenth. The so separated oil is distilled to such extent as may be desired.

Twentieth. rlhe so obtained distillate is finished for burning oil (kerosene), it may be, in any known or suitable way, with or without (best without) furt er treatment with sulfuric acid, say by subjecting it (l) to the well known Canadian treatment, which consists in (a) agitation with caustic soda lye and litharge followed by settling, (c) decanting, and (d) washing with water, and afterward (2) toa treatment in the known way with Florida clay (fullers earth) or the like by (a) agitation. settling, and (c) decanting; or the oil can be filtered through Florida clay or the like.

rllwenty first. The residue of ie light stream naphtlia bottoms, after separation of burning oil distillate therefrom, is distilled to dryness, or to the desired extent short ef dryness; and the so obtained distillate is utilized as pressure still stock. being supplied to a suitable still for distillation therein under the high pressure herein above men- Jtioned.

Twenty second. The residue obtained in rerunning the light stream burning oil distillate is distilled to dryness, or to the desired extent short of dryness; and the so is manufactured) in view of subsequent operations to which said distillate is to be subjected.

Twenty fourth. The so obtained distillate (light end of heavy stream) is operated upon for motor spirit- (or other light product), burning oil distillate and pressure still stock as herein above described for the light stream.

Twenty fifth. The residual portion of the heavy stream (after removal of its said light Iend) is distilled as long` as the distillate is the so obtained'distillate is utilized as pressure still stock.

Twenty seventh. The residue'of the original oil operated upon which remains in the pressure still at the close of the high pres-- sure run, and the residues of thehigli pressure distillate which remain as colte, or near coke, are disposed of as may be preferred.

Twenty eighth. The gasesan-d` incondensible vapors of distillation are disposed of as may be preferred.

l/Vhere parallel products are obtained it `is Well to mix them with each other, in order to simplify the procedure and plant. The mixture would then be operated upon as herein above described for the corresponding light stream product. Thus, for example, it is well to mix the heavy stream burning` oil distillate with the light streain'burning oil distillate and to operate upon the mixture as described for the latter. lt is probably ad: vantageous to distil the light Vstream naphtha bottoms separately; but if so desired, said bottoms could be mixed With the residual portion of the heavy stream (after removal of their motor spirit hydrocarbons)l or with the heavy stream burning oil distillate; and the resulting mixture in either case could be operated upon as herein above described in respect to the light stream naphtha bottoms. Residues from different sources from which burning oil hydrocarbons have been removed. can be mixed before distilling them to dryness, or to such lesser extent as may be preferred.

1Where crude petroleum is distilled in the same establishment it may be expedient to mix some of the products of such distillation and some of the products vof the high pressure distillation With each other, and

thereafter to operate upon the respective mixtures as herein abovedescribed:` for the corresponding products of thehigh pressure distillation. Thus, for example, the light stream might vvell be mixed with crude naplitha obtained either in distilling the crude petroleum or in rerunning the mixed naphtha-burning-oil-gas-oil distillate of the crude oil run (or with crude naphtha obtainedy in both these/modes) and the mixture could then be operated' upon as described for said light stream. The burning oil distillate from either or both streamsof high pressure distillatemay ywell be mixed vc ith (either or both) the Water' White burning oilldistillateof the crude oil run and the burning oil distillate from rerunning the mixed: naphtha-burning-oilgas-oil distillate of the crude oil run; and the so obtainedmixture could then be operated' upon as described forfthe light stream burning oil distillate. 1Residues of distillatesfof the crude oil' run and the high pressure run respectively ivhich remain after removal of the burning oil hydrocarbons therefrom could be mixed andthe mixture distilled for pressurestill stock. Also, if itl shouldV be so desired, theheavy streamnaphtha bottoms and the light stream naphtha bottoms (either or each of them) couldv be added to the mixednaphtha-bui'ning-oilgasoil distillate of the crude oil run, or even to the Water White burning oil distillate thereof.

It is considered best, in the high pressure distillation, to form the return condensate under the still` pressure, and to condense the remaining vapors as distillate under atmospheric pressure; but the condensation of all or any part of the said distillate may be effectedl under the still pressure, if preferred; and the formation of return condensate under a reduced: pressure is not necessarily excluded.

Additions can beinade at will to the foregoing' procedure within the scope of the invention; and parts of the said procedurecan be used Without employing other parts thereof.

Thus, according` to one modification ofsaid procedure, oil composed of gas oil or fuel oil hydrocarbons' which have been obtained as residue in distilling burning oil' distillate (either a Water White distillate or the succeeding mixed naphtha-burning-oil-gas-oil distillate or both) or as distillate in distilling a heavier distillate of the crude oil run (or Which have been obtained ineach of these Ways) is operated upon as herein above set forth in respect to the heavier of the aforesaid distillates from rerunning burning oil distillate or the like; but there is a special advantage in using this heavier distillate rather than the material from Which it would be derived. Furthermore, in accordance With this modiiication, any other suitable oil can be operated upon as herein above et torth, even crude petroleum or an undistilled residue thereof; but, in order to lessen the coa-L ing oit the still bottom in the high pressure distillation, it is better to employ a distillate oil.

..1`a ;eoi'dii1g to another inodilication, the vapors evolved in a high pressuie d'ftillation, wherein the conditions with condensation within the still are other than those hereinabove set are cooled outside the still in the form ot an upwardly inclined stream of the character herein above set fi'irth for formation otl return condensate, the procedure otherwise being herein above set forth.

ficcording to a third modilication, the vapors evolved in distilling a suitable oil under high` pressure are not cooled onL e the still in the 'term et an ui'iwardly inclined stream of the character herein above set forth; but return eenden is :termed in any other known or .itable mode, with such regulation, however, ci the cooling therefor that the onward passing vapors, to be condensed as distillate, have the composition herein above set tort-h.

According to a fourth modilication, the vapors which pass over to be condensed distillate s herein above set forth and which have the compositioi'i herein above set forth, instead ot' being fractionated by contact with the walls ot numerous parall -l cooluie` iiipes, are partially condensed in any o,

ierY known or suitable mode, with such regulation et the coolingv as is herein above set :torthN There may, moreover, be a series oit two or more partial condensations by contact with the walls or numerous parallel cooling gjiipcs, or otherwise.

,ficcording to a titth inoi'liticatiini, the h iavier oit the distillates obtainei'l aforei.l in rorunning burning oil dist'llate or being subjected to distlllation under superatmospheric pressure under the special condititons herein above set forth, is distilled in any other ai'ipropriato way at decomposing temperatures under .iperatinospheric pressure, as, ttor example, in any mode in which petroleum has heretofore been so distilled.

specification.

l igures l to 9 ci the accompanying draw ings illustrate, by way of example, one torni et apparatus in accordance with the invention and l() and 1l are diagrams ot typical procedures.

il? 1 is a side view oft the still end ot t' e apparatus, the View being" partly in section and partly in elevation. Y

2 a similar view oi the condenser end of the apparatus, the views oining each other at the line A.

Fig. 3 is a partial view ol the apparatui. in plan, the line A being located as in Figs. il and 2.

Fig. 4t is a partial view in side elevation oit the still and its setting which form part ot said apparatus. 1 Y

5 is a vertical cross section oi" said still and its setting, the lett halt ot the view on line 5 of Fig. i and the right halt on line 5C.

litigi;L 5 is a central vertical section, broken away in the middle and on an enlarged seal of a partial condenser,y .vhich 'tornis part oi he apparatus Fig. i' is a view ot said partial condenser `with its cover removed, the upper halt olf the -view in plan and the er halt in horizontal section on line ZU ot Fig. 2 partly broken away on line i r t3 and 9 are detail views ol a damper ariangemensJ ttor certain air inlets.r one oi" which appears at l) in Fig l.

Fig. 'lil shows a mode ot obtaining pressure still stock and other products trom Crude petroleum without the aid ot pressure distillation.

` 5. l1 shows a procedure whereby motor spirit, burning oil (kerosene) and a heavier oil suitable Ylor pressure still stock are obgrate and ash pit g, is located in said pounds per square inch above atmospheric pressure at decomposing temperatures is up held by lugs Z) secured thereto and restingl `upon the tops of columns e, 'whose bottoms rest upon the base CZ of the still setting.

An open topped fire chamber e, with re, base al under one end of the still a. and is separated by the bridge wall 7L from an open topped heating flue z' underlying the remainder of said still and leading to the down take j; which communicates with a chimney, not shown. The walls 7e make contact with still o; at a considerable distance below said lugs. They protect the 'intermediate overlying portions of the still from the lire gases.

At Z m are doors for fire chamber and ash pit, respectively. At a is a peep holer At p are bolts passing through foot flanges of the columns o for anchoring1 them to base d. At fr and a are recesses in base d.

Art the bottom of flue are gas burners t in the form of pipes perforated on top at short intervals throughout the greater part of their length and supplied with gas from gas line u through valved' connecting pipes o and with air from air line w through valved connecting pipes They extend each of them through an open ended tube y. The underlying air Adues .e have perfor-ated roof plates 2 and open ended tubes 3 for admission of air. Dampers for regulating the air admission would be provided on tubes 3. In the arrangement of Figs. 8 and 9 the stationary cap BX on tube 8 is provided with air inlet openings and intermediate cut-off portions 3, and carries the movable disk 3, which is pivoted on the cap and is provided with. correspondingair inlet openings and intermediate cut-off portions.

Two false bottoms d and in still a, one a short distance above the other, are each of them constituted by plates hinged at G to the still wall and lapped (Fig. 1) one upon another at their adjacent margins. Said plates can thus be turned up for cleaning out the sediment (colte) which collect-'s on the false bottoms and on the true bottom of the still.

At 7 are manholes. The charging line 8 has a valved branch pipe 9; which is turned (the `fittings serving as hinges) in order to insert the outer end through the adjoining manhole when the still ais to be supplied with oil.

The vapor pipe 10 connects with a safety valve 11. The escape pipe 1 2 (open at its outer end) extends therefrom through the overlying roof (not shown) or to whatever place may be desired. ln order to protect the safety valve 11 from the heated vapors in normal operation, it is desirable to inter1- pose a trap or U-bend 110 (Fig. 3) between the vapor pipe 10 and the safety valve 11 and to lill such trap with heavy oil, in order thus to form a liquid seal in said trap. The valved pipe 111 (F ig. l.) is provided for drawing off the oil from said trap when desired. The invention is not concerned with these arrangements.

The valved pipe 13 extends inside the still nearly to the bottom and is for removing the liquid which remains in the still at the close of each run. p

A steam line 14.- communicates with the vapor space of still a through a valved branch 15 for letting steam into the still at the close of each run. Dry steam is insured by allowing the steam to escape temporarily through valved blow-off 16.

The still top is exposed to the atmosphere, say to the extent of about a third of the periphery of the still, in order to form, from a portion of the vapors, condensate which is returned to the oil in distillation by directly dripping into the same or by running down the still walls. The exposed area can be increased or diminished by varying the brickwork 1'? or any non-conducting mate rial. The ends of the still may well be provided with non-conducting jackets 18.

The vapor pipe 10 would best be of small diameter, say about four inches, more or less, and of considerable length, say about eighty feet, more or less. It is exposed to the atmosphere for cooling in order to form, from a portion of the vapors, condensate which is returned to the oil in distillation. r:The surface area of such a pipe would be about eighty four square feet and its cubic contents about seven cubic feet. The cooling area of a still havingthe dimensions given above would be about four hundred and twenty square feet, if one-third of its periphery (excluding the ends) should be exposed to the atmosphere. The cubic contents of the still itself would be over three thousand cubic feet. Said pipe 10 is inclined upward from the still; so that condensate formed in said pipe willv1 on its way to the still, flow under and in cont-act with the outwardly flowing vapors. Extended opportunity is thus afforded for an interchange of hydrocarbons between condensate and vapors; and a better separation of hydrocarbons of different boiling points from each other is in consequence effected.

itt its outer end the vapor pipe 10 is connected by the cross pipe 19 and branch pipes 9.0 with the tower 21 for partially condensing` the vapors supplied thereto. In each pipe 2O there is a vapor throttling device 22, in the form as shown of a hand operated valve, best of needle type. Automatically operated valves are not necessarily excluded, but are not desirable.

Piping of three-quarters of an inch in diameter suffices tor pipes 20, and is advantageous in view ot the small size ot valve 22 which it is desirableV to employ.

The vapor condensing tower 2l consists (Fig. 6) of an upright cylinder (say six feet in diameter by thirteen feet in length) with tube sheets 222 near its top and bottom respectively, and also with numerous pipes 23 open at both ends and secured at the ends in said tube sheets, say 84 pipes of four inches diameter and eleven feet long. The pipes 20 open into the lower part of the space around pipes 23, and the vapor outlet pipe 24 leads from the upper part of the same space.

From the bottom of the same space leads a distillate draw-oitppe 25; which includes a trap 26 and which is immersed `for most of its length in the cooling water ot' tank 27.

At the top of vapor condensing tower 21 there is an adjustable valve, composed ot a stationary plate 28 and a movable plate 29, each ot them provided with air exit ports in the form of slots that register more or less with one another when the valve is more or less open and are out of registry when the valve is closed. At 30 is a stationary spacing ring surrounding the movable plate 29, and at 31 a stationary top ring which overlaps the margin of said movable plate 29. A bolt 32 passingthrough holes in plates 29 and 2S is tapped into disk 33; which rests upon the top ot post 34, fastened by its flanged base to the upper iue sheet 222. At- 35 are washers and at 36 a nut for the bolt 32.

The lever 37 fulcrumed on bracket 38,

which is fast on the tower 21, has a slot and pin connection with an arm 39, which is 'fastened to the movable valve plate 29. At 4() are stops for restricting the movement.

Near the bottom the tower has air inlet ports 4l (say three sets oi? tour holes two inches in diameter) and slides 42, movable in ways 43, tor regulating` the amount of air admitted.

The root 44 supported above the valve plates 28 and 29 at such height that air, escaping from the tower cylinder 2l, can pass out into the surrounding atmosphere.

The vapor pipe 24 is connected with a condenser pipe 45 immersed for most of its length in the cooling water of tank 27 and terminating in a distillate draw-ofl 450 distinct from the draw-off 25. Each of these draw-oils is provided with a valve. lVater is supplied to tank 27 by valvecl pipe 46; which discharges into the wide splash pipe 47 openinginto the tank 27 .near the bottom. The water escapes by the valved overflow pipe 48. For each of the pipes 25 and 45 there is a box or tee 49 provided with a valved pipe 50 tor conducting gas or uncondensed vapors away.

From the cross pipe i9 a valved pipe 5l leads to a discharge line which is connected by valved pipe 53 and a lower level discharge line 54, with a coil 55 in the cooltanlr that has a valved water supply pipe 57 and a valved water outlet pipe 58. The pipe lil connecte with the same coil 55 through the line 54.

From a point on the vapor pipe 10 intermediate the still a. and vapor condensing tower 2l a valved by-pass 59 leads around the tower 2l to the water cooled condenser pipe 45.

The valves oit various pipes are marked 60. Supports vlior the various parts are pro vided as may be necessary or expedient. At 6l is a platform for supporting the tank 27. At 62 a bracket is shown 'tor upholding the upper level discharge line 52 and the therewith connected pipes. .at 63 and 64 are beams for upholding the tower' 2l. At 65 are blocks under the ends ot beam 64. At 650 is a pressure gage.

Charging line S, discharge line 54 and other lines transverse to the length of still o are employed, in order that they may serve a number of stills placed side by side. The column at the right oi. Fig. 5 is shown with a bracket on each side at the top in order that it may receive lugs l) ot adjoining stills.

rllhe still a may be supplied with about 15,7 50 gallons oit oil through the charging line 8 and its branch 9, the cover of the ad jacent manhole 7 being temporarily removed. The said cover is replaced; and the still being now entirely tight the valve in by-pass 59 is opened and the valve in vapor pipe l() beyond its junction with said bypass 59 is closed. The valves in the gas and liquid outlets ot coolingpipe 25 and condenser pipe 45 are open. The valves belonging to the steam branch .l5 are closed,

is also the valve in pipe 13.

The temperature ot' the still n, and its contents is then raised gradually by lires in lire chamber e and at gas burners t until oil without water appears at the liquid outlet from condenser 45. .be vapor throttling valves 22 (one or botb or"A them) are now opened. and also the valve in vapor pipe 10; the valve in by-pass 59 is closed; and the heating is continued until oil appears at the liquid outlet 'from cooling pipe 25.

The vapor throttling valves 22 are then both ofi them closed; and the pressure in the still o; is allowed. to accumulate until the pressure gage 650 indicates approximately pounds per square inch above atmospheric pressure.

The vapor throttling valves 22 are then both oi them opened gradually and to an at least approximately equal extent. They may well be opened to such an extent that with said pressure ot 75 pounds the vapors passing said valves will form distillate at a rate somewhat under one and seven-tenths per cent per hour of the original still charge (say an average oi about l'iour and "fourtenths gallons in all of distillate per minute from both pipes 25 and l5 for a still charge of 15,750 gallons).

Distillationis then carried on with such regulation oi the still lires as to maintain thestill pressure as nearly as possible at 75 pounds gage pressure.

The evolved vapors are partially con densed in the vapor space above the oil in distillation; and the uncondensed vapors are further partially condensed in the vapor pipe 10. The condensate from both oit these partial condensations is returned to the oil in distillation; and an extended interchange oitl hydrocarbons takes place between the onward kflowing vapors and the returning condensate inthe vapor pipe 10, the more volatile constituents of the condensate being vaporized and carried onward, and the less volatile constituents of the vapors being condensed and returned to the still. By effecting a partial condensation in the vapor space of the still the heat of the oil in distillation, and of the still and its setting aswell, tends to prevent excessive variations in the volume oi' condensate formed, in consequence of variations in the currents of air coming into contact with the exposed top of the still, notwithstanding the fact that a large and compact body of vapors exists in said space. On theother hand, by the additional partial condensation of vapors between the more closely approached heat conducting walls oit vapor pipe 10 and by the extended opportunity for interchange oi hydrocarbons between Vcondensate and the vapors as eX- plained, a more efiicient separation of hydrocarbons is obtained than by a partial condensation in the vapor space alone. This separation in vapor pipe 10 is proportionately more efficient, in consequence ofthe delivery thereto of vapors which have been previously cooledv in the vapor space of still a.

Itis advantageous to lessen the cooling in the vapor pipe 10 so far as consistent with eiiiciency, for one reason because the iiuids (vapors or condensate, or both) exert a corroding action on the walls of said pipe, So great is this corrosion that all parts of the vapor pipe 10 should be examined periodically and renewals made as may be required.

Another reason, `which applies when, as is most convenient, the cooling is effected by exposure to the atmosphere, is that with such cooling the formation of condensate in vapor pipe 10 is apt to vary more than in the vapor space of the still. By having a relatively small volume of vapors in said pipe 10 the influence of such variation is made small.-

For both of these reasons it is advantageous to employ a vapor pipe 10 oi small diameter, the smaller in general the better, consistently with a tree passage therein oi the vapors and condensate in opposite directions.

lt may be observed in passing that (as shown) there is an absorption oi' heat by the expanding vapors in the pipes 20 near the upper end of pipe 10 and that this would tend to lower the temperature in the upper end of the pipe 10, in so far at least as it may by conduction abstract heat :from the wall oi' said. pipe 10.

After passing the throttling valves 22, the 'vapors enter the lower part oi' the tower 21, in the space (Fig. (l) between the tube sheets 222 outside ot the cooling` pipes 23. @n opening the air inlet and air exit ports, by suitably adjusting slides i3 and plate 29, the heat in pipes 23 induces upward currents of air. The vapors are cooled by flowing in contact with the walls of these numerousparallel pipes 23; which walls are interposed between the currents oit' said vapors and ol the aeriforin cooling agent respectively. As shown, said vapors are outside and the cooling agent inside oi said pipes; but similar cooling could be obtained by a reversed arrangementr in which the cooling air should ilow over the outside of numerous parallel pipes and the vapors inside the same.

The condensate which forms in'tower 21 escapes by the distillate draw-oill pipe 25 and is cooled by the water in tank 27.

.The uncondensed vapors from tower 21 pass by vapor pipe 211 to the water cooled condenser pipe 45. Vapors remaining uncondensed and uncondensible gas escape by the pipes 50 and are delivered to be burned as fuel in burners t or are otherwise disposed of, as may be preferred.

Distillation under high pressure should not be carried so liar as to become dangerous; and it can be arrested whenever desired. Firing is then discontinued; and the pressure in the still a is allowed to fall, the evolved vapors continuing to pass over to the tower 21.

When this pressure has fallen as low as desired (say to about fifty pounds, more or less, per square inch above atmospheric pressure) the valves in pipe 13 are opened; and the throttle valve 22 are closed. The pressure in the still then forces the fluid (liquid and aeriform) contents oi? the still through pipe 13, line 54 and coil 55 to any appropriate receiver (the aeriform contents being condensed in large part at least in said coil 55). When the still pressure has thus been suiliciently reduced (say to about ten pounds, more or less) steam is introduced through branch 15 into the still a (pipe 13 remaining open) until practically all of the hydrocarbon vapors have been expelledv The steam is then shut off; the valves in pipe 18 are closed; and when the still has cooled oil, it is thoroughly cleaned, inspected and (if necessary) repaired preparatory to a new run.

The valves in pipes 51, 52 and 58 leading by way of line 54 to coil 55 are not normally opened. laid pipes are provided as a relierl line, should it be necessary at any time to reduce the pressure in the still a quickly.

During a run, if any defect at all serious should appear either in the still or vapor pipe, the lires should be drawn, the still emptied, and proper repairs made before again charging the still with oil for a new run.

ln a run 'performed with the apparatus described on gas oil or fuel oil of specific grav ity 0.8488 under a superatmospherio pressure in the still a of about seventy live pounds per square inch with suoli throttling of the vapors at the valves 22 that distillate from both pipes 25 and 45 equal to about sixty and seven-tenths per cent. of the original still charge was collected in thirty siX hours, the observed temperatures of the oil in distillation ranged from 6960 F. to 7360 F., rising gradually and steadily, average 7180 F.; those of the vapors leaving still a at Athermometer 60 ranged from 5280 F. to 5780 F., average 5580 F. while at thermometer 67 (Fig. 8) ust beyond the divide which separates distillate hydrocarbons from those returned to the still a the temperatures ranged from 4820 F. to 4980 F., varying irregularly, average 4650 F. The temperatures were observed at the vclose of every hour.

The temperatures at the top of pipe 24 (thermometer G8) ranged from 2670 F. to 8900 F., average 3410 F. Y

The residual material in the still at the close of the run amounted to about thirty six and threewtenths per cent. of the original charge, loss about three per cent.

.fr samole of this total distillate (obtained o' fairly representative samples of distillate from each of the pipes specific gravity of about 0.7857) was subjected to a distillation assay and showed:

The vapors leavingl vapor pipe 10 in this d a content of about ten per cent. (measured in liquidstate) of hydrocarbons with boiling' points above 5180 F.

The distillate (heavy stream) from par tially condensing these vapors, drawn oii from tower 21 through pipe 25, amounted to about twenty four and five-tenths per cent. of the original charge of still a. lt had a speciio gravity of about 0.8156. A fairly representative sample of it was suljected to a distillation assay and showed:

Dist-illate up to 8020 F., about 4.5% Distillate 3020 F. to 4100 F., about 14.0% Distillate 4100 F. to 5180 about @il in assay tias.; at 5180 F., about 28.5% .ll-oss (by difference), about 1.5%

rlotal 100.0%

rlhe distillate (light stream) from the draw-oil of water cooled condenser' 45 amounted to about thirty siX and two-tenths per cent. of the original cha eje of still ait had a specific gravity of about 0.7641. A fairly representative sample of it was sub Vhile the two streams of high pressure distillate, the light stream from condenser 45 and the heavy stream from tower '71 can be operated upon, or disposed of, as may be preferred, the invention includes the s ject-ion of them to the operations, or an appropriate part at the least of the operations, set forth in the earlier part of the present specilication for obtaining' (1) a light product (such as motor spirit), burning oil (kerosene), pressure still stock. and (4) residual materials which may be (in whole or in part) in the form of colte, from two streams of high pressure distillate.

For the performance of these operations ordinary agitators and stills will suilice; and the t'oreg'oing` description will enable those skilled in the art to per form the saine. lt may he added,however, in respect to the high pressure distillate from the aforesaid njas oil or fuel oil of specific gravity 0.8488 that about live pounds of ordinary concentrated sulfuric acid containing' 92.5% to 03% by weight of sulfuric inonohydrate (101280,) to each forty two `a'allons of oil would be saitable for giving' the mild treatment inentiou to the light stream high pressure distillate (including the light end the heavy stream) and about seven pounds of the saine description of acid for the treatment of the mixed burning' oil distillates from the light stream naphtha bottoms and the heavy stream naphtha bottoms respectively.

The approximate yields from such gas oil or fuel oil would be as follows in per centages or the oil charged into still a at the beginning of the high pressure run.

Motor spirit, specific gravity say 0.7889, about 21.9% Burning' oil (kerosene), yspecific gravity say 0.8109, about 21. 9% Pressure still stock, specilic gravity say 0.8762, about 12.4% Coke and loss in working up high pressure distillate .(by difference),

1n a distillation assay about eighty per cent. of saidmotor spirit would d-istil over below 302O F. and about seventeen fandfvetenths per cent. thereof between 3027 F. and 3950 F. (flask dry at last mentioned temperature) loss in assay about two and fivetenths per cent.

The said burning oil (kerosene) would be water whi'tegwith a hash `test of Labout 110O F.; and in distillation'assay about ninety five and five-tenths per cent. of it would distil over below 518 F.y (oil in assay flask about three and ve-tenths per cent. at last mentioned temperature); loss in yassay about one per cent.

ln a concurrent application, No. 7 96,310, filed October 20, 1913, on which lPatent 1,221,790 was granted Apr. 3, 1.917, I have described and claimed some ol. the matter exhibited herein. The application for the present patent is to be regarded as a continuation of said concurrent application in so far as it properly may be so regarded.

' l claim herein as my invention lor discovery:

1. In the art of obtaining products from petroleum, wherein hydrocarbons boiling above 518O F. are collected in admiXture with those boiling below 518o F., form of burning oil (kerosene) distillate from distilling crude petroleum under relatively low pressure (as atmospheric pressure, for example), and are afterward separated from lighter components of said burnin@ oil (kerosene) distillate, by partial distillation of this latter under relatively low pressure, and are yet later distilled at decomposing temperatures under superatmospheric pressure of more than thirty pounds per square inch, the improvement which consists in subjecting the residual oil from partially distilling said in lthe-- burning oil (kerosene) distillate to distillatin 'under lrelatively low pressure, with collection of distillate that boils above 518O F., anddin distilling this last mentioned distillate at decomposing temperatures undersuperatmospheric pressure oi more than thirty pounds'per square inch, substantially as described.

` 2. ln the art or' obtaining products from petroleum, wherein hydrocarbons boiling above 518o F. are collected in admixture with those boiling below 518O F., in the form of burningoil (kerosene) distillate from distilling crude petroleum under relatively low pressure (as atmospheric pressure, `for example), and are afterward sep arated from lighter components of said burning oil (kerosene) distillate, by partial distillation of this latter under relatively low pressure, and are yet later distilled decomposing temperatures under superatmospheric pressure of more than thirty pounds per square inch, the improvement whichcomprises (l) treating said burning oil (kerosene) distillate with sulfuric acid, (2)"-s'ep`a`rating vreaction products, (3) partially distilling the acid treated oil, (l) sub jecting residual oil from which lighter co1nponents have thus been, separated to distillation under relatively low pressure, with collection of distillate that boils above 518O F., and distilling` this last mentioned distillate at decomposing temperatures under superatmospheric pressure of more than thirty pounds per square inch, substantially as described.

In the art of obtaining products ironi petroleum, wherein hydrocarbons boiling above 518o F.V are subjected, in the iiorni ot a compact body of petroleum with an original volume of not less than iive thousand gallons, -to distillation at decomposing telnpcratures lunder super-atmospheric pressure o it' more than thirty pounds per square inch, accompanied by a cooling of so evolved vapors 'for formation o1' condensate which is returned to the oil in distillation and by a fun ther fcooling of the then remaining vapors for formation of condensate which is collected as distillate, the improvement which consists in reducing the average temperature o'l so evolved vapors in their compressed state at least as low as 518o F. and not below 410 F. for formation of so returned condensate,

b coolino` said va )ors rst in the va )or space overlying said body oi: petroleiun through contact of the same with the exposed top of the sill and afterward in an outside space, whose cubic content is less than one and a half per cent. ol? the original volume of the said body off petroleum, by means oi. a relatively long travel of the vapors between air cooled walls that are relatively close together as compared with like conditions in the still, in such manner that the vapors at their exit from the still are between one hundred degrees F. and two hundred degrees F. below the contemporaneous temperatures of the oil in distillation, and are between forty degrees F. and one hundred and forty degrees F. cooler at the place where said formation of return condensate cea than they are at their said exit from the still, the vapors which pass onward from the place just mentioned being further cooled for formation of condensate which is collected as distillate, substantially as described.

l. ln the art of obtaining prod ucts fro .i petroleum, wherein hydrocarbons boiling above 518 F. are subjected, in the form of a. compact body of petroleum with an origi nal volume of not less than live thousand gallons, to distillation in a still of elongated cylindrical form at decomposing temperature under supera-tmospheric pressure of more than thirty pounds per square inch, accompanied by a cooling of so evolved vapors for formation of condensate which is returned to the oil in distillation and by a fur'- ther cooling of the then remaining vapors for formation of condensate which is collect ed as distillate, the improvement which consists in reducing the average temperature of so evolved vapors in their compressed state at least as low as 518 F. and not below 410G F. for format-ion of so returned condensate, by cooling said vapors first in the vapor space overlying said body of petroleum through contact of the same with an area of exposed still top equa-l to about one-third he periphery of said still and afterward in an outside space, whose cubic content is less than one and a half per cent. of the original volume of the said body of petroleum, by means of a relatively long travel of the vin pors between air cooled walls that are relatively close together as compared with like conditions in the still and that have an area of exposed surface equal to between ten per cent. and thirty per cent. of the exposed arca of said still top, the vapors which pass onward from the place where said formation of return condensate ceases being further cooled for formation of condensate which is collected as distillate, substantially as de scribed.

5. n apparatus for obtaining products from petroleum, which apparatus comprises (first) a still in the form of an elongated cylinder with a capacity of not less than one thousand cubic feet and with walls suflicicntly strong to withstand a superatmospheric pressure of more than thirty pounds per square inch at oil decomposing temperatures, (second) means for heating said still and its liquid contents to oil decomposing temperatures, (third) an outside partial con denser which receives vapors from said still and returns condensate thereto and in which the vapors are cooled by a relatively long travel between air cooled walls that are relatively close together as compared with like conditions in the still, (fourth) means whereby the contents of said still and said outside partial condenser can be held under a superatmospheric pressure of more than thirty pounds per square inch, and (fifth) condensing means which receive vapors from said outside partial condenser and which discharge the therein formed condensate as distillate, the improvement which not only includes all of the foregoing parts, but which comprises the three following features in addition thereto, namely: the exposure of the top of said elongated cylindrical still to the atmosphere over an area equal to about one-third of its periphery, (2) an interior construction of said still which allows the return to the oil in distillation of ccndensate formed in the vapor space of the said still, and (3) a construction of said outside partial condenser wherein the compressed vapors are cooled to form return condensate as aforesaid in such manner that the cubic content thereof is less than one per cent. of the still capacity and that its air cooled walls have an exposed surface equal to between ten per cent. and thirty per cent. of said exposed areaA of the still top, substantially as described.

6. In the art of obtaining products from petroleum, wherein hydrocarbons boiling above 5180 F. are subjected, in the form of a compact body of petroleum with an original volume of not less than five thousand gallons, to distillation at decomposing temperatures under superatmospheric pressure of more than thirty pounds per square inch, accompanied by a cooling of so evolved vapors for formation of condensate which is returned to the oil in distillation and by a further cooling of the then remaining vapors for formation of condensate which is collected as distillate, the improvement which consists in forming part at least of the so returned condensate by passing the compressed vapors over air cooled walls outside of the still in such manner that from the commencement of the outside cooling said vapors have the form of a single elongated stream, inclined upwardly at an -oblique angle and restricted in diameter about as far as may be consistent with the free passage of the compressed vapors and the condensate in opposite directions, said stream being less than six inches in diameter in any case and upward of one hundred diameters in length in any case, and being exemplified by a four-inch stream eighty feet long in distilling a body of petroleum with an ori nal volume of about fifteen thousand gallons at decomposing temperatures under a superatmosphoric pressure ot' about seventy live pounds per square inch, and the vapors that pass onward from the place where the tmfmation of return condensate ceases being further cooled 'tor formation of condensate which is collected as distillate, substantially as described.

7. In apparatus for obtaining products from petroleum, which apparatus comprises (first) a still with a capacity of not less than one thousand cubic feet and with walls su'fliciently strong to withstand a superatinospheric pressure of more than ythirty pounds per square inch at oil decomposing temperatures, (second) means for heating said still and its liquid contents to oil decomposing temperatures, (third) an outside partial condenser which receives vapors from said still and returns condensate thereto and in which the vapors are cooled by a relatively long travel between air cooled walls that are relatively close together' as compared with like conditions in the still, (fourth) means whereby the contents .of said still and said outside partial `condenser can be held under a superatmospheric pressure of more than thirty pounds per squareinch, and (fifth) condensing means which receive vapors from said outside partial condenser and which discharge .the therein formed condensate as distillate, the improvement which not only includes all the toren going parts, but which comprises the two following features in addition thereto, namely: (l) the construction of said outside partial .condenser, wherein the compressed vapors are cooled to form return condensate as aforesaid, in the form of a single elongated pipe, inclined upwardly at an oblique angle and restricted in diameter about as `liar as may be consistent with the -tre-e passage oit the compressed vapors and the condensate in opposite directions, said pipe being less than six inches in diameter in any case and upward of one hunderd diameters in length in any case, and being exemplified by a four-inch pipe eighty feet long for a still with a capacity of about three thousand cubic feet, and (2) a connection of said pipe with the vapor space of the still which allows the vapors to enter said pipe at the temperature which they have on leaving the still, substantially as described.

8. ln the art of obtaining products from petroleum, wherein hydrocarbons boiling' above 5180 l?. are subjected, in the form of a compact body of petroleum with an original volume of not less than five thousand gallons, to distillation at decomposing temperatures under superatmospheric pressure of more than thirty pounds per square inch, accompanied by a cooling of so evolved vapors for formation of condensate which is returned to the oil in distillation and by a :further cooling of the then remaining vapors for formation of condensate which is collected as distillate, the improvement which consists in reducing the average tempera tures ot so evolved vapors in their compressed state at least as low as lSOl and not below Li100 F. or 'formation olf so returned condensate, by cooling said vapors first in the vapor space overlying sait body of petroleum to between one hundred degrees F. and two hundred degrees i". below the contemporaneous temperatures oi the oil in distillation, through contact ot the vapors with the exposed top of the still, and alterward in an outside space, whose cubic content is less than one and a halt per cent ot the original volume of said body ot petroleum through a further temperature interval of between forty degrees F. and one hundred and forty degrees F. by travel ot the compressed vapors over air cooled walls in such manner that from the commencement of the outside cooling the vapors have the form of a single elongated stream, inclined upwardly at an oblique angle and restricted in diameter about as liar as may be consistent with the free passage or" the conipressed vapors and the condensate in opposite directions, the said stream being less than six inches in diameter in. any case and upward of one hundred diameters in length in any case, and being exemplilied by a tourinch stream eighty feet long in distilling a body of petroleum with an original volume of about fifteen thousand gallons at decomposing temperatures under a superatmospheric pressure of about seventy-five pounds per square inch, and the vapors that pass onward from the place where the formation et return condensate ceases being further cooled -for formation oi' condensate which is collected as distillate, substantially as described.

9. ln the art of obtaining products from petroleum, wherein hydrocarbons boiling above 518 F. are subjected, in the ,torni of a compact body of petroleum with an original volume of not less than live thousand gallons, to distillation in a still of elongated cylindrical form at decomposing temperatures under superatmospheric pressure oli more than thirty pounds per square inch, accompanied by a cooling ot so evolved vapors for formation of condensate which is returned to the oil in distillation and by a further cooling ot the then remaining vapors for formation oi condensate which is collected as distillate, the improvement which consists in reducing the average temperature of so evolved vapors in their compressed state at least as low as 5180 F. and not below 4100 F. for formation olf so returned condensate, by cooling said vapors first in the vapor space overlying said body of petroleum through contact of the same with an area of exposed still top equal to about one-third the periphery of said still, and afterwardL in an outside space, whose cubic content is less than one and a half per cent. of the original volume of said body of petroleum, by means of a relatively long travel of the vapors between air cooled walls that are relatively close together as compared with like conditions in the still and that have an area of exposed surface equal to between ten per cent. and thirty per cent. of the exposed area of said still top in such manner that from the commencement of the outside cooling the vapors have the form of a single elongated stream, inclined upwardly at an oblique angle and restricted in diameter about as far as may be consistent with the free passage of the compressed vapors and the condensate in opposite directions, the said stream being less than six inches in diameter in any case and upward of one hundred diameters in length in any case, and being exemplified by a four-inch stream eighty feet long in distilling a. body of petroleum with an original volume of about fifteen thousand gallons at decomposing temperatures under a superatmospheric pressure of about seventy five pounds per square inch, and the vapors that pass onward from the place where the formation of return condensate ceases being further cooled for formation of condensate which is collected as distillate7 substantially as described.

10. In apparatus for obtaining products from petroleum, which apparatus comprises (first) a still in the form of an elongated cylinder with a capacity of not less than one thousand cubic feet and with walls sufficiently strong to withstand a superatmospheric pressure of more than thirty pounds per square inch at oil decomposing temperatures, (second) means for heating said still and its liquid contents to oil decomposing temperatures, (third) an outside partial condenser which receives vapors from said still and returns condensate thereto and in which the vapors are cooled by a relatively long travel between air cooled walls that are relatively close together as compared with lilre conditions in the still, (fourth) means whereby the contents of said still and saidoutside partial condenser can be held under a superatmospheric pressure of more than thirty pounds per square inch, and (fifth) condensing means which receive vapors from saidoutside partial condenser and which discharge the therein formed condensate distillate, the improvement which not only includes all the foregoing parts, but which comprises the four following features in addition thereto, namely:

(l) the exposure of the top of said elongated cylindrical still to the atmosphere over an area equal to about one-third of its periphery, (2) an interior construction of said still which allows the return to the oil in distillation of condensate formed in the vapor space of the said still, (3) a construction of said outside partial condenser wherein the compressed vapors are cooled to form return condensate as aforesaid in the form of a single elongated pipe, inclined upwardly at an oblique angle and restricted in diameter about as far as may be consistent with the free passage of the compressed vapors and the condensate in opposite directions, said pipe being less than six inches in diam- 8o eter in any case and upward of one hundred diameters in length in any case, and having a cubic content of less than one per cent. of the still capacity and an area of exposed wall surface equal to between ten per cent. and thirty per cent. of said exposed area of the still top, and being exemplified by a four-inch pipe eighty feet long for a still with a capacity of about three thousand cubic feet, and (d) a connection of said pipe with the vapor space of the still which allows the vapors to enter sait pipe at the temperature which they have on leaving the still, substantially as described.

1l. In the art of obtaining products from petroleum, wherein hydrocarbons boiling above 518 F. are subjected te distillation at decomposing temperatures under superatmospheric pressure, accompanied by a cooling of so evolved vapors for formati n of condensate which is returned to the oil in distillation and by a furtlrr the then remaining vapors for forni: of condensate which is collected as distil late, the improvement which consi 'ts in performing said cooling for formation of return condensate in such manner that the then remaining vapors contain a relatively large proportion of hydrocarbons boiling above 410 F. (as compared with customary crude motor spirit of the pressure distillation type) and at least an appreciable amount of hydrocarbons boil above 518 F. but a proportion nevertheless of the latter which is smaller than customary in burning oil (kerosene) distillate, that to say, not less than thirty live per een'. (measured in liquid state) of hydrocarbon-f boiling above L110 F. and not more than twenty live per cent. of those boiling` above 518 F., a typical composition for said vapors (subsequently condensed as distillate as aforesaid) comprising about forty five per cent. of hydrocarbons boiling above 410 F. and about ten per cent. above 518 F., substantially as described. n

12. In the art of obtaining products from petroleum, wherein hydrocarbons boiling abovelo F. are subjected to distillation at decomposing` temperatures under superatmospheric pressure, accompanied by a coolino of so evolverA vapors forformation of condensate which is returned to the oil in distillation and by a further cooling of the then remaining' vapors for formation of condensate which is collected as distillate, the improvement which consists (first) in performingv said cooling 'for formation of return condensate in such manner that the then remaining vapors contain a relatively large proportion of hydrocarbons boiling l above t100 F.. (as compared with customary crude motor spirit of the pressure distillation type) and at least an appreciable amount of hydrocarbons boiling' above lilo F. but a proportion nevertheless of the latter which is smaller tnan customary in burning oil (kerosene) distillate, that is to say, not less than thirty five per cent. (measured in liquid state) of hydrocarbons boiling` above Zl1()O F. and'not.. more than twenty live per cent. of those boiling1 above 518O F., a typical composition for said va-- pors (subsequently condensed asdistillate as aforesaid) comprisingabout forty five per cent. of hydrocarbons.boiling above @i100 F. and about ten )er cent. above 518O lll., and (second) in separating said lrydroca bons (Whose vapors are thus condensed as distillate) into oils of different gravities' in such manner that one at least of said oils boils in part below and in part above 3020 F. and practically all of it below 410O F., substantially as described. y

18. ln the art of obtaining` products from petroleum, wherein hydr carbons boiling` above 5180 l?. are subjected to distillation at decomposing temperatures under sniper.- atmospheric pressure, accompanied by a cooling of so eveloved vapors for formation of condensate which is returned to the oilin large proportion of hydrocarbons boilingr etl above 11.00 l?. (as compared with customary crude motor spirit of the pressuredistillation type)V and .at least an appreciable amount of hydrocarbons boiling` above 51So il". but-a proportion nei/eri less of the latter which is smaller than customary in burn ing;` oil (kerosene) distillate, that is to say,

Vnot less thanthirty live per cent. (measured.

in liquid state) of hydrocarbons boiling above 4100 ld. and not more than twenty five percent; of those boiling above 518 F., a typical composition for said vapors(subse quently condensed as distillate as aforesaid) comprising about forty five per cent. of

- (fifth) in distilling' the acid treat hydrocarbons boiling` above 410O F. and about ten per cent. Vabove 5180 F., and (second) in separating said hydrocarbons (Whose vapors are thus condensed as distill ate) into oils of different gravities in two staoes inthe first of which an oil that boils in partv above L11()o F. but is practically from hydrocarbons boiling above 5180 F. is obtained as one of the products,and in the second of which this oil is partially distilled with collection of distillate that boils practically all of it below t100 F.,

improvement Which consists (iirst) in per-V formingsaid cooling for formation of returnl condensate in such manner that the then remaining' vapors contain a relatively large proportion of hydrocarbons boiling above 4109i?. (as compared with customary crude motor spirit of the pressure Vdistillationtype) amountof hydrocarbons boilingabovc 518? F. but a proportion.nevertheless ofthe latter which issmaller than customary in burning oil (kerosene) distillate, that'is tosay, not less than thirty five per cent.- (measured in liquid state) of hydrocarbons boiling); above i-100 F. and not more `than twenty five per cent. of thoseboiling aboi'fe'lOV F., a typical` composition for said vapors (subsequently condensed as distillatev as aforesaid) comprising about fort `tive per cent. of hydrocarbons boiling-.above i100 F. and about ten per cent. above 5180 ll.. (second) in separating said hydrocarbons (whose vapors are thus condensed yas distillate) into oils of different gfravities insuchinanner that one at least of said oilsboils in part above i100 'I but ispractically free from hydrocarbons boiling abovewliO it.. (third) in subjecting. this oil to treatment with. sulfuric acid,

(fourth) in separatinrgy reaction products. ed oilV in snr'h manner that oils ol difiere s are obtained, the lighter atleast or them as distillate. (sixth) in subjectingra so obtained heavier oil to treatment with sulfuric acid, and (seventh) in separating reaction prodn ucts,V the hydrocarbons composing this Iheavier oil being thus :subjected to sulfuric acidi in admixture with lighter hydrocarbons and again after separation Vof the latter therefrom., substantially as described..

15. In the art of obtaining products from petroleum, wherein hydrocarbons boiling and aty least an appreciable condensate Wl .h is returned to the oil in dis l anu by a further cooling1 of the ien reni ring vapors 'for formation of condensate ich .is collected as distillate, the

improvement which consists (rst) in performing said cooling tor formation of return. condensate in such manner that the then tenir ing; vapors contain a relatively large proportion ot hydrocarbons boilingabove l-lGO n. (as compared with customary crude rnotor spirit ci" the pressure distillation type) and least an appreciable arno 1-1L of hydrocarbons boiling,` above 518O but proportion nevertheless ol the latter which is smaller than customary in burning oil (kerosene) distillate, that is to say, not less than thirty live per cent. (measured in liquid te) et hydrocarbons boilingl above t100 F. and not more than twenty tive per cent. or' t se boiling above 518C F., a typical i `for said vapors (subsequently condensed as .distillate as aforesaid) cornprisingr abou" live per cent. olf hydrocarbons boiV above 41.0 F. and about ten per cent. abev 518 Il., and (second) in mictionally condensin,nsaid vapors in such rn .ner that light str am distillate, Which boils in part above 1GO but is practically i'iree from hydrocarbonsboiling above 518o ll., is ob d with a stream of heavier distilte, substantially as described. 13S. Vln the ot obteining` products 'from ielroleum. .vherein hydrocarbons boiling above tilt?" l? `1e subjeited to distillation at decoinposin .Grupera ures under supercompositi arinospheric pr Je, accompanied by a c cling? of so evolved vapors lor formation o i condensate which is ret .rn-ed to the oil in ,l l hstflation an: cr cooling' ot the then reinsinir j Y torination oi conder-sate which is c .,.ectcd as distillate, the

improvement ivliirh consists (lirst) in performing' said cooling;

formation ot resuch manner that the vapors contain a relatively on ot hydrocarbons boiling- 'is compared with customary oi the pressure distilla lez-st an appreciable amounlnl? hi, rocarhons b nlinr` above 518O F het a pr oortion nevertheless ont the latter which is smaller oil (lrorosone) distillate. that less tha thm' Y'c `per cent. .liquid e 41d@ l?. ano not no than twenty .five per cent. ci thos^ bollino` above 5180 F., a typin tor said vapors (subsequently condensed as distillate as aforesaid) comprising/2 about forty live per cent. of

ian (sistemr :y in burning is to say, not (measured in hydr carhons boiling above hydrocarbons boiling above ell()o and about ten per cent. above 5180 ll., (second) in ifractionally conuensing said vapors in such manner that a light stream distillate, which boils in Y 't above llO il. but is gra..ctirally free troni hf drocarbons boiling,Y above 5180 F. is obtained alono' with a stream ot heavier distillate, (third) in subjecting this light stream distillate to treatment With sulfuric acid, (fourth) in separating reaction products, (lilith) in distilling` the acid treated oil in such manner that oils ol? ditl'erent gravities are obtained, the lighter at least of them as distillate, (sixth) in subjecting` a so obtained heavier oil to treatment with sulfuric acid, and (seventh) in separating` reaction products, the hydrocarbons composing this healer oil being;` thus subjected to sull'ru'ic acid in adinizrture with lighter hydrocarbons and again utter separation ot the latter therefrom, substan-- tially as described.

17. ln the art of obtaining products 'f petroleum, wherein hydr carbone boiling,r above 518O l?. are collected in adrniirture vith those boiling` beloiv 5180 F., in the torna ol3 high pressure distillate 'from subiecti hydrocarbons that boil above 5180 F. to distillation at decomposing temperatiures under superatmospheric pressure in excess of thirty pounds per square inch, and are afterward separated from lighter coinponents of said high pressure distillate., by p artial distillation ol' this latter under relatively louT pressure, and are yet later distilled at decomposing); temperatures under superatmospheric pressure ot more than thirty pounds per square inch, the improvement which consists in subjecting' residual. oil from partially distillingg` said high pressure distillate to distillation under rel 'vely low pressure, with collection. ot distillate boiling above 518O F., and in distillinga this last mentioned distillate at delcomposing;A temperatures unl'ler superatinospheric pres sure ol more than thirty pounds per square inch, substantially as described.

18. In the art ot obtainingv pr ducts troni oetroleum.` wherein hydrocarbons boilinaj above 5180 are collected in aduiinture with those boilingbelon7 5180 ll.. in. the lorrn ot high pressure distillate Jrom srcd'eet tf; hydrocarbons that boil above 5180 F. to dia tilla tion at decomposnc temperatures under sru'ieratmospheric for ssure in excess et thirty pounds per square inch. and are attervrard separated .trom lighter components ot said high pressure distillate, by partial dise tillation ot this latter under relatively lo-y pressure, and are yet later distilled at decomposing tenmeratures under supeiatniospheric pressure oi' more than thirty pounds per square inch, the improvement which comprises (1) treating' said high pressure distillate with sulfuric acid, (2) separating reaction products, partially distilling the acid treated oil, (1l) subjecting residual oil from which lighter components have thus been sepan-ated to distillation under relittixfely low pressure, with collection of distillate that boils above 5180 F., and (5) distillilig this lust mentioned distillate wat decomgesing teiiiperetures under supei'atmosplieic pressure o'i more than thirty pounds 10 pei' square inch, subststiitelly as described.

In testimony whereof I affix my signature.

HORACE l. CHAMBEBLAN. 

